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WO1997025448A9 - Methode d'enrichissement du trona - Google Patents

Methode d'enrichissement du trona

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Publication number
WO1997025448A9
WO1997025448A9 PCT/US1996/020191 US9620191W WO9725448A9 WO 1997025448 A9 WO1997025448 A9 WO 1997025448A9 US 9620191 W US9620191 W US 9620191W WO 9725448 A9 WO9725448 A9 WO 9725448A9
Authority
WO
WIPO (PCT)
Prior art keywords
trona
separating
impurities
separation
electrostatically
Prior art date
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Ceased
Application number
PCT/US1996/020191
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English (en)
Other versions
WO1997025448A1 (fr
Filing date
Publication date
Priority claimed from US08/583,879 external-priority patent/US5736113A/en
Application filed filed Critical
Publication of WO1997025448A1 publication Critical patent/WO1997025448A1/fr
Publication of WO1997025448A9 publication Critical patent/WO1997025448A9/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

Links

Definitions

  • the present invention relates generally to the beneficiation of sodium carbonate and, more particularly, trona.
  • saline minerals are recognized as being commercially valuable. For example, trona, borates, potash and sodium chloride are mined commercially. After mining, these minerals typically need to be beneficiated to remove naturally occurring impurities.
  • trona Na 2 CO 3 .NaHCO 3 .2H 2 O
  • trona is commonly used to make soda ash, which is used in the production of glass and paper.
  • Naturally-occurring trona, or crude trona is found in large deposits in the western United States, such as in Wyoming and California, and also in Egypt, Kenya, Botswana, Cambodia, Venezuela and Turkey.
  • Crude trona ore from Wyoming is typically between about 80% and about 90% trona, with the remaining components including shortite, halite, quartz, dolomite, mudstone, oil shale, kerogen, mica, nahcolite and clay minerals.
  • the glass and paper making industries generally require soda ash produced from trona having a purity of 99% or more.
  • wet beneficiation processes have been used. Such processes generally involve crushing the crude trona, solubilizing the trona, treating the solution to remove insolubles and organic matter, crystallizing the trona, and drying the trona which may subsequently be calcined to produce soda ash.
  • the crude trona can be calcined to yield crude sodium carbonate, which is then solubilized, treated to remove impurities, crystallized and dried to produce sodium carbonate monohydrate.
  • U.S. Patent No. 4,341,744 discloses a dry beneficiation process which is less complex and less expensive than the above-described wet beneficiation process.
  • Such a dry beneficiation process generally includes crushing the crude trona, classifying the trona by particle size, electrostatically separating certain impurities, and optionally magnetically separating other impurities.
  • Such a process can yield trona having up to about 95% to 97% purity, depending on the quantity and type of impurities present in the crude trona ore.
  • the present invention is embodied in a process for recovering a high-purity saline mineral from an ore containing the saline mineral, such as trona, and impurities.
  • the process generally includes separating a first portion of impurities from the trona by an electrostatic separation method at a temperature between about 25°C and about 45°C. More preferably, the electrostatic separation is conducted at a temperature between about 30°C and about 40°C, and even more preferably is conducted at a temperature of about 35°C.
  • the weight recovery of trona electrostatically separated from a feedstream containing trona and impurities according to the present invention is at least about 75%.
  • the amount of iron impurities removed from a feedstream containing trona and impurities by conducting electrostatic separation according to the present invention is at least about 80%.
  • the efficiency of iron impurities removal and trona recovery from a feedstream containing trona and impurities according to the present invention is at least about 65%.
  • the process includes separating a second portion of impurities from the trona by a density separation method which may occur before or after electrostatic separation of the first portion of impurities from the trona at a temperature between about 25°C and about 45°C.
  • the density separation step can include air tabling or dry jigging to separate impurities having a different density than the trona.
  • the second portion of impurities removed by the density separation step may comprise shortite.
  • the density separation step occurs after electrostatic separation.
  • the process includes separating a second portion of impurities by a magnetic separation step.
  • the magnetic separation step may occur before or after the step of electrostatic separation at a temperature between about 25°C and about 45oC.
  • the magnetic separation step occurs before electrostatic separation.
  • a process is provided for the beneficiation of trona from a feedstream of trona having impurities.
  • the process generally includes the steps of sizing the feedstream of trona into a first size fraction and a second size fraction, separating the first size fraction into a first recovered portion and a first impurity portion by electrostatic separation at a temperature of between about 25°C and about 45oC, and separating the second size fraction into a second recovered portion and a second impurity portion by a wet separation method.
  • the electrostatic separation of the first size fraction is conducted at a temperature between about 30°C and about 40oC, and more preferably at a temperature of about 35°C.
  • the process may further include calcining the trona to form sodium carbonate, the calcining step occurring after the electrostatic separation step.
  • the process includes separating a first portion of impurities by a magnetic separation step, subjecting the nonmagnetic portion recovered from the magnetic separation step to electrostatic separation at a temperature between about 25°C and about 45°C, which separates the "dirty" trona from the "clean” trona. Thereafter, the "clean" trona may be calcined to produce sodium carbonate. The sodium carbonate may then be subjected to a density separation step.
  • saline mineral refers generally to any mineral which occurs in evaporite deposits.
  • Saline minerals that can be beneficiated by the present process include, without limitation, trona, borates, potash, sulfates, nitrates, sodium chloride, and preferably, trona.
  • the purity of saline minerals within an ore depends on the deposit location, as well as the area mined at a particular deposit.
  • the mining technique used can significantly affect the purity of the minerals. For example, by selectively mining, higher purities of saline minerals can be achieved.
  • Deposits of trona ore are located at several locations throughout the world, including Wyoming (Green River Formation), California (Searles Lake), Egypt, Kenya, Venezuela, Botswana, Cambodia and Turkey (Beypazari Basin). For example, a sample of trona ore from Searles Lake has been found to have between about 50% and about 90% by weight (wt.%) trona and a sample taken from the Green River Formation in Wyoming has been found to have between about 80 and about 90 wt.% trona.
  • the remaining 10 to 20 wt.% of the ore in the Green River Formation sample comprised impurities including shortite (1 to 5 wt.%) and halite, and the bulk of the remainder comprises shale consisting predominantly of dolomite, clay, quartz and kerogen, and traces of other impurities.
  • Other samples of trona ore can include different percentages of trona and impurities, as well as include other impurities.
  • the present process is directed to processes for the beneficiation of saline minerals and, in particular, the beneficiation of trona.
  • preferred embodiments of the present invention will be discussed with reference to trona.
  • the intended scope of the present invention includes processes for the beneficiation of saline minerals more generally.
  • the present process includes removing a first portion of impurities from a feedstream of trona having impurities by an electrostatic separation method.
  • Electrostatic separation methods are based on subjecting the ore to conditions such that materials of different electrical conductivities separate from each other.
  • electrostatic separation can be used to separate trona from impurities having a higher electrical conductivity, such as shale, mudstone, or pyrite. It should be appreciated, however, that electrostatic separation could also be used to separate impurities that have a lower electrical conductivity than the saline mineral being recovered.
  • One embodiment of the present invention for beneficiation of trona having impurities includes the step of electrostatically separating a first portion of impurities from the trona which is at a temperature of between about 25°C and about 45°C. It has been surprisingly found that by conducting electrostatic separations in this temperature range significant increases in efficiencies can be obtained. Any known electrostatic separation technique can be used for this step of the present invention, including differential electrification, as disclosed in U.S. Patent No. 4,341,744, which is incorporated herein by reference in its entirety. As discussed in the above- identified patent, saline mineral ore particles are first differentially electrified and then separated into a recovered stream from an impurity stream by various electrostatic separation processes, including, conduction or conduction in conjunction with ion bombardment.
  • beneficiation of trona from a feedstream of trona having impurities is conducted by electrostatically separating a first portion of impurities from the trona at a temperature of between about 25°C and about 45°C, more preferably at a temperature between about 30°C and about 40°C, and most preferably, at about 35°C.
  • the feedstream of trona having impurities can be heated to the identified temperatures prior to and/or during separation.
  • the feedstream of trona may be heated to the desired temperature in a standard drying oven prior to differential electrification.
  • both the feed bin and the roll may be heated during electrostatic separation.
  • the ambient temperature during the separation can be maintained at a high enough temperature to meet the above-noted temperature requirements.
  • electrostatic separation at a temperature between about 25°C and about 45°C can remove at least about
  • the trona weight recovery (weight of trona recovered/weight of trona in the feedstream) from the electrostatic separation at a temperature between about 25°C and about 45°C is between about 60% and about 95%, and more preferably, between about 70% and about 90%, and most preferably about 80%.
  • electrostatic separation at a temperature between about 25°C and about 45°C increases the efficiency of iron removal and trona recovery.
  • the efficiency (in percent) may be quantitatively measured as follows: ((weight percent of iron assay of feedstream - weight percent of iron assay of recovered product) /weight percent of iron assay of feedstream) x percent of trona recovered x 100.
  • conducting electrostatic separation at a temperature of about 35°C resulted in a reduction of the iron (Fe 2 O 3 ) assay by about 83% and the trona recovery was 80%, which equals an efficiency of about 65%.
  • the impurity stream from a first pass of an electrostatic separation process can go through a scavenger step to improve the overall recovery.
  • the scavenger step recovers a trona-containing portion of the impurity stream from the first pass through electrostatic separation and combines it with the recovered stream to increase the overall yield of the electrostatic separation step or otherwise cycles it to other steps in the process.
  • the recovered stream from the first pass of the electrostatic separation can go through one or more electrostatic cleaning steps to further remove impurities from the recovered stream and improve the purity of the final product.
  • a second portion of impurities may be separated from the feedstream of trona by a density separation step.
  • Density separation methods are based on subjecting an ore to conditions such that materials of different densities physically separate from each other. Thereby, certain impurities having a different density than the desired trona can be separated.
  • the density separation step of the present invention is most preferably a dry process, however, wet density separation processes, such as heavy media separation, can be used as well. In dry density separation processes, the need for processing in a saturated brine solution, solid/brine separation, and drying of the product is eliminated. Any known density separation technique could be used for this step of the present invention, including air tabling or dry jigging.
  • the density or gravity separation step may occur after the electrostatic separation step.
  • density separation is conducted by subjecting an ore to conditions such that materials of different density separate from each other.
  • the mineral stream having materials of varying densities is then separated by a first or rougher pass into a denser and a lighter stream, or into more than two streams of varying densities.
  • trona is recovered in the lighter stream.
  • impurities that are removed during the density separation step of the present invention include shortite having a density of 2.6, dolomite having a density of 2.8-2.9, and pyrite having a density of 5.0. Each of these is separable from the trona ore because of differences in density from trona.
  • the density separation step can remove at least about 10 wt.%, more preferably about 50 wt.%, and most preferably about 90 wt.% of the heavy impurity.
  • the present process may further include a magnetic separation step which subjects the ore to conditions such that materials of different magnetic susceptibility separate from each other into a recovered stream and an impurities stream.
  • the magnetic separation step can be accomplished by any conventional technique, such as induced roll, cross-belt, or high intensity rare earth magnetic separation methods.
  • induced roll is used in the present invention for the finer fractions and high intensity rare earth magnets are used for the coarser fractions.
  • typical impurities can be removed during the magnetic separation step include shale which has a higher magnetic susceptibility than trona.
  • an induced roll magnetic separation technique can remove at least about 5 wt.%, more preferably about 50 wt.%, and most preferably about 90 wt.% of the shale from the material being treated by magnetic separation.
  • the trona-containing ore or trona can be crushed to achieve liberation of impurities prior to the separation steps.
  • the crushing step of the present invention can be accomplished by any conventional technique, including impact crushing (e.g., cage or hammer mills), jaw crushing, roll crushing, cone crushing, autogenous crushing or semi-autogenous crushing. Autogenous and semi-autogenous crushing are optional because the coarse particles of ore partially act as the crushing medium, thus requiring less cost in obtaining grinding media.
  • impact crushing e.g., cage or hammer mills
  • jaw crushing roll crushing
  • cone crushing autogenous crushing or semi-autogenous crushing
  • autogenous and semi-autogenous crushing are optional because the coarse particles of ore partially act as the crushing medium, thus requiring less cost in obtaining grinding media.
  • trona is typically soft, these methods are suitable for use in the present process. In addition, these two crushing methods allow for the continuous removal of crushed material and high grade potentially saleable dust.
  • trona is sized into size fractions prior to the separation steps. Each size fraction is subsequently processed separately.
  • the narrower the range of particle size within a fraction the higher the efficiency of removal of impurities.
  • a large number of fractions will increase the efficiency, but may increase the cost of the overall process.
  • the use of between 3 and 10 fractions has been found to be acceptable.
  • the number of fractions is between 4 and 10, and more preferably, the number of fractions is 10.
  • Any conventional sizing technique can be used for the present process, including screening or air classification.
  • the fractions typically have the following particle size ranges : 6 x 8 , 8 x 10 , 10 x 14 , 14 x 20 , 20
  • +100 mesh fractions may be processed by any dry process described herein and the -100 mesh may be processed by any wet method described herein, or sold without processing as they are enriched in the sizing process.
  • the trona is dried prior to the separation steps set forth above.
  • the drying step removes surface moisture from the trona to better enable the trona to be separated. Drying can be accomplished by any conventional mineral drying technique, including rotary kiln, fluid bed or air drying.
  • the ore can be dried to less than about 2%, and preferably to less than about 1% surface moisture content.
  • it is preferred that the trona is not raised to such a temperature for such a period of time that it is calcined. In the case of trona, the drying temperature should remain below about 40°C to avoid calcination.
  • a de-dusting step is added to the basic beneficiation process to remove fines before the electrostatic separation step.
  • De-dusting can be particularly important before electrostatic separation because the dust can otherwise interfere with the effective electrostatic separation.
  • Such a de-dusting step can be conducted before, during or after one or more of the crushing, sizing and/or density separation steps.
  • the fines produced during the processing of trona are relatively high purity trona and are useful in several industrial applications.
  • trona recovered by de-dusting can have a purity of greater than about 94%, preferably greater than about 96% and preferably greater than about 98%. Fines can be collected in de- dusting steps by use of a baghouse, or other conventional filtering device, and sold as purified trona without further processing.
  • combination dry and wet processes for the production of trona are provided.
  • the dry processes can include any known or hereafter developed processes for the dry beneficiation of ores containing trona. Such processes can include density separation, magnetic separation, and/or electrostatic separation at a temperature between about 25°C and about 45°C.
  • the wet processes can include any process which includes dissolution and crystallization, such as those disclosed in commonly assigned U.S. Patent Application Serial No. 08/373,955, filed January 17, 1995, and U.S. Patent Application Serial No. 08/544,135, filed October 17, 1995, both of which are incorporated by reference in their entirety herein.
  • a wet separation method of the various embodiments of the present invention includes a dissolution and crystallization process. Such a process takes advantage of the fact that the solubilization and crystallization of saline minerals results in more pure crystals because impurities are excluded as crystals are formed after solubilization.
  • the product recovered thereby is highly pure and can contain greater than about
  • such product has less than about 0.05 wt.% iron. More preferably, the iron content is at most about 0.02 wt.% and even more preferably at most about 0.01 wt.%.
  • saline mineral crystals are dissolved in water or an unsaturated saline solution.
  • trona the sesquicarbonate form of sodium carbonate
  • anhydrous sodium carbonate calcined trona
  • water is driven off, and the saline mineral crystallizes.
  • the water can be driven off by heating the solution.
  • such a process can be expensive and time-consuming due to the energy required to heat the water and the amount of time required to fully dry the crystals.
  • trona is first calcined to produce anhydrous sodium carbonate crystals which are added to a saturated sodium carbonate brine solution.
  • anhydrous crystals go into solution and recrystallize, they crystalize in the monohydrate form if the temperature is between about 35°C and about 112°C. Accordingly, there is a continuous crystallization process which tends to significantly reduce the impurities in the crystals. Crystals can then be recovered from the brine solution.
  • U.S. Patent No. 2,887,360 issued May 19, 1958 (Hoekje).
  • a process for the production of trona from a feedstream having impurities includes the steps of separating a first portion of a feedstream of trona into a first recovered portion and a first impurity portion by a dry separation method, and separating a second portion of the feedstream of trona into a second recovered portion and second impurity portion by a wet separation method.
  • the second portion may comprise particles having a particle size larger than about 100 mesh and more preferably, larger than about 65 mesh.
  • the dry separation method is selected from the group consisting of density separation, magnetic separation, electrostatic separation processes as described herein, and combinations thereof.
  • the wet separation method can be a dissolution and crystallization process.
  • this embodiment can further include the step of calcining the trona to form sodium carbonate.
  • the process for the production of saline mineral from a feedstream having impurities is provided.
  • This embodiment includes the steps of separating a first portion of impurities by a dry separation method, and separating a second portion of impurities by a wet separation method, wherein at least about 15 wt.% of said feedstream is processed by said wet separation method.
  • the dry separation method is selected from the group consisting of density separation, magnetic separation, electrostatic separation processes as described herein, and combinations thereof.
  • the wet separation method includes a dissolution and crystallization process.
  • the weight percent process by said wet separation process is at least about 20%, and more preferably at least about 30%.
  • this embodiment can further include the step of calcining the trona to form sodium carbonate.
  • Carpco electrostatic separator having a 10-inch roll. To minimize the variables in the tests, the revolutions per minute were held constant at 100 rpm and the position of the top electrode was unchanged (full pinning) . The effective voltage was evaluated visually and no benefit was observed in using less than the maximum attainable without arcing.
  • Two different bottom electrodes were evaluated in the tests of splits 1-13, the first being a combination electrode consisting of a 1-inch aluminum rod with a nichrome wire suspended on one side, the other electrode being a very flattened hollow oval which provided a broad surface for lifting.
  • the trona splits were heated to the above-noted temperatures in a standard drying oven and, to minimize the cooling of these splits during separation, the feed bin and the electrostatic separator roll were heated to slightly higher than the desired temperature with a heat gun. Surface temperatures were measured with an infrared thermometer, and split temperatures were measured with a thermal couple. The calibration of the infrared thermometer and the thermocouple were checked using boiling water. The data generated from the foregoing beneficiation process is shown in Tables 1-2. As can be seen from the

Abstract

Méthode d'enrichissement du trona, provenant d'un courant d'amenée contenant du trona et des impuretés, par un procédé de séparation par voie sèche, c'est-à-dire de séparation d'une première partie des impuretés du trona par effet électrostatique à une température comprise entre 25 °C et environ 45 °C. Cette méthode d'enrichissement du trona peu également comprendre la séparation des impuretés du trona par d'autres procédés de séparation par voie sèche tels que la séparation par densité, la séparation magnétique et la séparation granulométrique.
PCT/US1996/020191 1996-01-11 1996-12-18 Methode d'enrichissement du trona Ceased WO1997025448A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
US08/583,879 US5736113A (en) 1996-01-11 1996-01-11 Method for beneficiation of trona
US583,879 1996-01-11

Publications (2)

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WO1997025448A1 WO1997025448A1 (fr) 1997-07-17
WO1997025448A9 true WO1997025448A9 (fr) 1997-10-09

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US6173840B1 (en) * 1998-02-20 2001-01-16 Environmental Projects, Inc. Beneficiation of saline minerals
US6428759B1 (en) * 2000-05-02 2002-08-06 Fmc Wyoming Corporation Production of feed liquors for sodium carbonate crystallization processes
US6667021B2 (en) 2001-09-12 2003-12-23 General Chemical Corporation Method for producing enhanced sodium carbonate crystals for making sodium bicarbonate
US7517509B2 (en) * 2004-03-31 2009-04-14 University Of Utah Research Foundation Purification of trona ores by conditioning with an oil-in-water emulsion
US7473407B2 (en) * 2004-11-19 2009-01-06 Solvay Chemicals Magnetic separation process for trona
WO2009062177A2 (fr) * 2007-11-08 2009-05-14 University Of Utah Research Foundation Systèmes et traitements pour produire du trona de pureté élevée
TR201105519T1 (tr) * 2008-12-22 2011-09-21 Solvay (Societe Anonyme) Sodyum karbonat ve sodyum bikarbonatın birlikte üretimi için işlem.
EP2399866A1 (fr) 2010-06-22 2011-12-28 Solvay SA Processus pour la production associée de carbonate de sodium et de bicarbonate de sodium
US9327233B2 (en) * 2010-09-14 2016-05-03 Tronox Alkali Wyoming Corporation Method of beneficiating and drying trona ore useful for flue gas desulfurization
WO2013092754A1 (fr) 2011-12-23 2013-06-27 Solvay Sa Procédé pour la coproduction de carbonate de sodium et de bicarbonate de sodium
BR102012008340B8 (pt) * 2012-03-19 2022-12-13 Steel Participacoes E Investimentos S A Processo e sistema para recuperação a seco de finos e super finos de minério óxido de ferro

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US3655331A (en) * 1969-06-06 1972-04-11 Intermountain Res & Dev Corp Production of sodium carbonate
US3802556A (en) * 1970-03-26 1974-04-09 Wintershall Ag Process for electrostatic dressing and/or working up of salt and mineral mixtures
US3835996A (en) * 1972-08-22 1974-09-17 Kali & Salz Ag Process for the electrostatic separation of clay containing crude potassium salts
US4341744A (en) * 1979-01-22 1982-07-27 Stauffer Chemical Company Soda ash production
US4375454A (en) * 1980-12-12 1983-03-01 Intermountain Research And Development Corporation Electrostatic enrichment of trona and nahcolite ores
US4512879A (en) * 1983-07-20 1985-04-23 Battelle Development Corp. Process for producing a metalliferous concentrate from a particulate feed material
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